Modelling and simulation of the Esbjerg pilot plant using the Cesar 1 solvent

Kvamsdal, Hanne M.; Haugen, Geir; Svendsen, Hallvard F.; Tobiesen, Andrew; Mangalapally, Hari Prasad; Hartono, Ardi; Mejdell, Thor

doi:10.1016/j.egypro.2011.02.036

Cited by 22 publications

(12 citation statements)

References 5 publications

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“…Compared with other simulation and experimental results, the simulated energy consumption locates in the same range (Abu-Zahra, Schneiders, Niederer, Feron, & Versteeg, 2007;Kvamsdal et al, 2011). The experimental results in the literature are closer to the simulated results than to results given here from pilot plants with similar configuration and operating conditions.…”

Section: Experimental and Simulated Results Comparisonsupporting

confidence: 53%

“…The equilibrium model is not only "economic" and "simple", but may be more suitable for the energy-related research in the pilot plant system (Abu-Zahra, Schneiders, Niederer, Feron, & Versteeg, 2007;Kvamsdal et al, 2011). The comparison of energy consumption for different solvents could only have meaningful results at each other's optimal operating conditions (Mangalapally et al, 2009).…”

mentioning

confidence: 99%

“…Several pilot plants have been established, and a series of tests have been carried out for design variables and process parameter evaluation (Wilson et al, 2004;Yokoyama, 2004;Dugas, 2006;Mangalapally et al, 2009;Kvamsdal et al, 2011). Process simulations of MEA-based solvent CO 2 capture through an absorption/stripping operation offer a valuable alternative method to help identify the key process variables and design parameters (Desideri & Paolucci, 1999;Abu-Zahra, Schneiders, Niederer, Feron, & Versteeg, 2007;Khan, Simioni, Van Zijll de Long, & Stevens, 2007;Kvamsdal et al, 2011). The ratio of solvent circulation rate to flue gas rate (L/G), identified as an important operation parameter for solvent based CO 2 capture process, has yet to be thoroughly scrutinized (Freguia & Rochelle, 2003;Hassan, 2005;Abu-Zahra, Schneiders, Niederer, Feron, & Versteeg, 2007).…”

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confidence: 99%

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Simulation of the Energy Consumption of CO2 Capture by Aqueous Monoethanolamine in Pilot Plant

Han¹,

Graves²,

Neathery³

et al. 2011

EER

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Monoethanolamine is a conventional solvent used for capturing carbon dioxide from coal fired power plants. Its stable performance makes it a good benchmark to explore other absorbent or technological processes. In this paper, process simulations based on Aspen Plus are conducted to identify how operating parameters influence energy consumption and efficiency for the carbon dioxide capture. Experimental results carried out in a pilot plant will be reported along with the comparisons to the simulated results. Comparative discussion against existing publications in the same area regarding the simulation validity is also carried out.

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Section: Experimental and Simulated Results Comparisonsupporting

confidence: 53%

mentioning

confidence: 99%

mentioning

confidence: 99%

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Simulation of the Energy Consumption of CO2 Capture by Aqueous Monoethanolamine in Pilot Plant

Han¹,

Graves²,

Neathery³

et al. 2011

EER

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“…However, in order to perform a detailed calculation of the gas-liquid mass and heat transfers, the characteristics of the column packing are required. These data have been retrieved from the Esbjerg Pilot Plant for CO 2 capture (Kvamsdal et al, 2011;Faber et al, 2011) and are presented along with some rate-based modeling assumptions in Table 1. Some chemical reactions occurring in the absorber and in the stripper are assumed to be at equilibrium, while other are kinetically limited.…”

Section: Model Descriptionmentioning

confidence: 99%

Influence of process operating conditions on solvent thermal and oxidative degradation in post-combustion CO2 capture

Léonard

Crosset

Toye

et al. 2015

Computers & Chemical Engineering

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Monoethanolamine thermal and oxidative degradation Process modeling Plant design Integrated experimental and modeling study a b s t r a c tThe CO 2 post-combustion capture with amine solvents is modeled as a complex system interconnecting process energy consumption and solvent degradation and emission. Based on own experimental data, monoethanolamine degradation is included into a CO 2 capture process model. The influence of operating conditions on solvent loss is validated with pilot plant data from literature. Predicted solvent consumption rates are in better agreement with plant data than any previous work, and pathways are discussed to further refine the model. Oxidative degradation in the absorber is the largest cause of solvent loss while thermal degradation does not appear as a major concern. Using a single model, the process exergy requirement decreases by 10.8% and the solvent loss by 11.1% compared to our base case. As a result, this model provides a practical tool to simultaneously minimize the process energy requirement and the solvent consumption in post-combustion CO 2 capture plants with amine solvents.

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“…One of the major disadvantages of post-combustion capture processes is the process energy requirements. The state of the art MEA is known to require 3.4-4 GJ/ton CO 2 (Liebenthal et al, 2013;Kvamsdal et al, 2011;Knudsen et al, 2009Knudsen et al, , 2007. However, some new solvents are claimed to reduce the regeneration energy requirement.…”

Section: Introductionmentioning

confidence: 99%

Density Calculations of Aqueous Amine Solutions Using an Excess Gibbs Based Model

Pinto

Knuutila

2019

Braz. J. Chem. Eng.

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Accurate representation of the physical properties of a solvent is essential for design and simulation of processes. Density and viscosity, for instance, have an important role in modelling and designing absorption and desorption towers. In the present work, a model to accurately calculate the density of aqueous amine solutions used in CO 2 capture was developed as a function of temperature and composition. The model is based on excess Gibbs energy functions, and in this work the functional form of the non-random two-liquid (NRTL) model was used. The model is able to accurately represent the density of the tested systems with deviations below 0.2% for most cases. The pure component density was calculated using the modified Rackett equation with the parameter Z RA as a function of the temperature and pressure of the system. The calculated deviation (AARD) for pure component density was below 0.09%.

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Modelling and simulation of the Esbjerg pilot plant using the Cesar 1 solvent

Cited by 22 publications

References 5 publications

Simulation of the Energy Consumption of CO2 Capture by Aqueous Monoethanolamine in Pilot Plant

Simulation of the Energy Consumption of CO2 Capture by Aqueous Monoethanolamine in Pilot Plant

Influence of process operating conditions on solvent thermal and oxidative degradation in post-combustion CO2 capture

Density Calculations of Aqueous Amine Solutions Using an Excess Gibbs Based Model

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